System for system for preparing high-purity taurine and salt

ABSTRACT

A system for preparing high-purity taurine and salt. The system can be used in an ethylene oxide process for producing taurine. The system includes an addition reaction device, an ammonolysis reaction device, an evaporation device, and a taurine salt concentrated solution collection device. The ammonolysis reaction device is provided with a metal salt inlet, the taurine salt concentrated solution collection device is connected with an ion exchange system for ion exchange, the ion exchange system is provided with an acid inlet, an adsorption solution outlet and an eluate outlet, the adsorption solution outlet of the ion exchange system is connected with a taurine extraction device, the eluate outlet of the ion exchange system is connected with a salt extraction device, and the ion exchange system is provided with a purified water inlet, an adsorption unit cleaning water outlet and an elution unit cleaning water outlet.

RELATED APPLICATIONS

The present application is a divisional of U.S. patent application Ser.No. 17/236,691, filed Apr. 21, 2021, which issued as U.S. Pat. No.11,578,037. The foregoing application is incorporated by referenceherein.

BACKGROUND

The present disclosure relates to a production method in a process forchemically synthesizing taurine, in particular to a method for producinghigh-purity taurine and salt (e.g., sodium sulfate or sodium chloride)by an ethylene oxide method, and a production system thereof.

Taurine (2-aminoethanesulfonic acid) is the most abundantsulfur-containing free amino acid in the body's cells. A chemicalsynthesis process route of taurine mainly includes an ethylene oxidemethod and an ethanolamine method, wherein preparation by the ethyleneoxide method includes three steps:

(1) using ethylene oxide as a starting material, performing an additionreaction of ethylene oxide and sodium bisulfite to obtain sodiumhydroxyethyl sulfonate (also known as sodium isethionate), wherein themain reaction is:

CH₂CH₂O+NaHSO₃→HOCH₂CH₂SO₃Na

(2) carrying out ammonolysis of the sodium hydroxyethyl sulfonate toobtain sodium taurate:

HOCH₂CH₂SO₃Na+NH₃→H₂NCH₂CH₂SO₃Na+H₂O

(3) adding sulfuric acid for acidification of the sodium taurate toobtain taurine and a salt:

2H₂NCH₂CH₂SO₃Na+H₂SO₄→H₂NCH₂CH₂SO₃H+Na₂SO₄

Chinese Patent Nos CN101508657, CN10158658, CN10158659 and CN101486669describe a method of obtaining taurine and sodium sulfate byneutralizing sodium taurate with sulfuric acid. After cooling, byfiltering a crystal suspension, a crude taurine product can be veryeasily obtained. However, the waste mother solution still containstaurine, ammonium sulfate and other organic impurities. These patentsalso provide feasible methods for further separating these componentsfrom the waste solution so as to implement economy of production andreduce discharge of wastes. However, since the materials are mixedtogether in the same mother solution, separation of the taurine, sulfateand the like is very difficult, the process design is complex, energy issimultaneously extracted, and cost of labor and the like is very high.Meanwhile, product purities of the taurine and the sulfate arerelatively low.

U.S. Pat. Nos. 9,428,450B2 and 9,428,451B2 and European Patent No.EP3133060B1 describe cyclic methods for producing taurine, including adetailed description of a principle and method of separating the taurinefrom sodium sulfate. Solubility of the sodium sulfate is the maximum ata temperature of 33° C. At a temperature between 33° C. and 100° C., thesolubility of the sodium sulfate is gradually and slightly reduced, butwithin a range of 0° C. to 33° C., the solubility of the sodium sulfateis sharply reduced. At a temperature of 40° C. or above, the sodiumsulfate is separated out in the form of anhydrous crystals; and at atemperature of 30° C. or below, the sodium sulfate is separated out inthe form of mirabilite (i.e., sodium sulfate decahydrate). Each timewhen the taurine is extracted, the temperature is controlled within arange of about 33° C., the taurine is extracted, and meanwhile, sulfateis prevented from being crystallized. The mother solution obtained afterextraction is evaporated and crystallized, and the sodium sulfate isseparated at a temperature of 70° C. to 95° C. The method mainlyutilizes different solubility characteristics of the sulfate and thetaurine at different temperatures to implement separation between thetaurine and the sodium sulfate. The operation process is very complex.Since several materials are in the same mother solution system, puritiesof the products obtained by separation are necessarily relatively low.

CN110683970A describes a method for removing a sodium sulfate solidimpurity from taurine. The method mainly is that the taurine isextracted from sodium sulfate using a deep-eutectic solvent preparationmethod. A deep-eutectic solvent is formed by utilizing monoethanolamineand the taurine, the sodium sulfate impurity is removed by filtering,and separation is carried out by utilizing a series of organic solventreextraction and the like so as to obtain pure taurine. Such methodintroduces many types of organic solvents, and is also relativelycumbersome to operate; an intermediate control point needs to be veryaccurate, and the industrialization difficulty is very high.

CN109020839A describes a recycling process for preparing taurine bycarrying out ammonolysis on sodium hydroxyethyl sulfonate. The contentof a taurine crude product is 90%, sodium sulfate is transformed into awater glass product (sodium silicate) with low levels of impurities, andan effect of solving a problem of processing the sodium sulfate isachieved. The process has the main problem that the process does notsolve the purity problem of the crude taurine product and the sodiumsulfate and is just a subsequent processing process for low-content,low-purity products.

From the above, the existing process for preparing the taurine by asulfuric acid neutralization method still has many defects in the aspectof separation and purification of the taurine and the sulfate, which aretypically require a complex separation process, low purities ofseparated products, low extraction rates and high extraction costs.Therefore, a process capable of preparing high-purity taurine andsulfate or other salts is needed.

SUMMARY

The present disclosure aims to provide a method and system for preparinghigh-purity taurine and salt, which are simple in process and low inproduction cost.

The present disclosure provides a method for preparing high-puritytaurine and salt that includes the following steps:

-   -   reacting ethylene oxide with bisulfite to generate isethionate;    -   carrying out an ammonolysis reaction on the isethionate and        ammonia as well as a metal salt;    -   carrying out evaporation to obtain a concentrated taurine salt        solution;    -   subjecting the concentrated solution to ion exchange in an ion        exchange system to obtain an adsorption solution with a main        ingredient of taurine;    -   separately collecting the adsorption solution, and extracting        the taurine from the adsorption solution;    -   eluting adsorbed metal cations by an acid, and separately        collecting the eluate; and    -   extracting the salt from the eluate or directly using the eluate        as a salt solution product.

In one embodiment, the bisulfite is sodium bisulfite, ammoniumbisulfite, potassium bisulfite or lithium bisulfite, particularly sodiumbisulfite or ammonium bisulfite. Suitable metal salts include any oneof, or a mixture of any two or more of, sodium hydroxide, potassiumhydroxide, lithium hydroxide, sodium carbonate, potassium carbonate,lithium carbonate, sodium sulfate, potassium sulfate and lithiumsulfate, particularly sodium hydroxide or sodium sulfate. Suitable acidsinclude sulfuric acid, hydrochloric acid, phosphoric acid, water-solublecarboxylic acid, and sulfonic acid, particularly sulfuric acid orhydrochloric acid.

In one particular embodiment, the ion exchange system includes anadsorption unit and an elution unit, and each unit is respectivelycleaned with purified water, and correspondingly obtained cleaning wateris respectively collected.

In some embodiments, when the ion exchange system is operating in anadsorbing state, the adsorption solution is collected when pH of asolution at an outlet of the adsorption unit is 4 to 10. When operatingin an eluting state, the eluate is collected when the pH of a solutionat an outlet of the elution unit is 2 to 8.

Preferably, metal cations which are at least equivalent in molar amountto that of residual isethionate anions are allowed to enter theadsorption solution.

In terms of the taurine, the concentration of the concentrated solution(in terms of taurine) entering the ion exchange system is, for example,10% to 35% (on a mass/volume basis, or % m/v).

The concentration of the acid added into the ion exchange system is, forexample, 5% to 35% (on a mass/volume basis).

In particular embodiments, the adsorbent used in the ion exchange systemis an ion exchange resin that adsorbs the cations (e.g., metal cations).

The step of extracting taurine from the adsorption solution can include,for example, the steps of: evaporation concentration, coolingcrystallization and solid-liquid separation. Cooling crystallization andsolid-liquid separation can be carried out at 5° C. to 30° C., and ataurine crude product obtained by separation has a taurine content ofover 95% (g/g) and a taurine purity of 98.5% or above.

The salt (e.g., sodium sulfate) can be extracted from the eluate in anevaporation crystallization mode, wherein the evaporationcrystallization is carried out at 60° C. to 125° C., and a salt crudeproduct obtained by separation has a salt product content of over 97%and a salt product purity of 98.5% or above.

On the basis of the preparation method, the present disclosure furtherprovides a system for producing high-purity taurine and salt, which canbe used in a process for producing taurine by an ethylene oxide method.The system includes, for example, an addition reaction device, anammonolysis reaction device, an evaporation device and a taurine saltconcentrated solution collection device. By way of example, (a) asuitable addition reaction device can include a reaction kettle orreaction vessel, heat exchanger, transfer pump, storage tank, etc.; (b)a suitable ammonolysis reaction device can include an ammonolysismaterial and batching tank, heat exchanger, transfer pump, storage tank,high temperature and high pressure heater, high pressure pump, and hightemperature and high pressure tower; (c) a suitable evaporation devicecan include a flash tank, heat exchanger, separator, transfer pump,storage tank, vacuum pump, etc.; and (d) a suitable taurine saltconcentrated solution collection device can included a storage tank,mixer, transfer pump, etc. The size and form of this exemplary equipmentcan be designed and adjusted according to the applicable requirementsand needs. The ammonolysis reaction device is provided with a metal saltinlet. The taurine salt concentrated solution collection device isconnected with an ion exchange system for ion exchange. The ion exchangesystem is provided with an acid inlet, an adsorption solution outlet andan eluate outlet. The adsorption solution outlet is connected with ataurine extraction device (e.g., as described in ¶ [0062]), and theeluate outlet is connected with a salt extraction device (e.g., asdescribed in ¶ [0062]). The ion exchange system is also provided with apurified water inlet, an adsorption unit cleaning water outlet and anelution unit cleaning water outlet. The cleaning water can beefficiently recycled. In some instances, the adsorption unit cleaningwater outlet is connected with the taurine salt concentrated solutioncollection device, and the elution unit cleaning water outlet isconnected with the salt extraction device.

Based on the above, the present disclosure relates to a method forproducing high-purity taurine and salt. Materials of these two targetproducts (taurine and salt) are efficiently separated in an ion exchangemode after the ammonolysis reaction. Strict separation of materialsystems is implemented, and moreover, extraction and purification areseparately carried out, so that the two target products of the taurineand the salt have very good crystal forms of crystallization, a finalextraction rate is greatly promoted, and the purities of the obtainedtaurine and salt are both very high, wherein the taurine crude productcan reach the content of 95% or above and the purity of over 98.5%, thesalt crude product can reach the content of 97% or above and can reachthe purity of 98.5% or above, and, after recrystallization, the contentof both the products is 99.5% or above.

In a conventional taurine production process, by taking a byproductsulfate as an example, the taurine and the sulfate exist in the samemother solution system, separation has to be carried out by utilizingthe solubility difference between the taurine and the sulfate, i.e.,when solubility of sodium sulfate is the maximum, firstly, the taurineis extracted, and then a solution containing a great amount of taurineand sulfate after extraction is subjected to concentration separation;generally, firstly, the sulfate is separated out at a high temperature,then cooling is carried out to a temperature of about 33° C. to extractthe taurine, and extraction is repeatedly carried out for many times.This process is very cumbersome to operate, and an extraction rate andproduct quality of the taurine are also seriously restricted. Obviously,all the materials exist in the same system and the materials are high inviscosity, resulting in a poor crystal form of crystallization of thesulfate, and thus, the sodium sulfate obtained by separation isrelatively low in purity. Meanwhile, it is inevitable that the taurinecrude product contains a great amount of sulfate, and it is alsoinevitable that the sulfate contains taurine, resulting in a difficultyof separating the taurine from the mother solution, and thus, theextracted taurine is relatively low in content and the yield is reduced.

Compared to the conventional production process, the preparation methodsdisclosed by the present disclosure are equivalent to extracting thetaurine from the high-purity taurine mother solution system andextracting the salt from the high-purity salt mother solution system,and is completely not related to interference brought to productseparation when two target products exist in the same maternal system,so that the processes for extracting two target products are simplified,the production cost is greatly reduced, and further, the automatic,intelligent and continuous design is also easier to implement in thewhole product production process.

BRIEF DESCRIPTION OF THE DRAWINGS

While the specification concludes with claims particularly pointing outand distinctly claiming the invention, it is believed that the inventionwill be better understood from the detailed description of certainembodiments thereof when read in conjunction with the accompanyingdrawings. Unless the context indicates otherwise, like numerals are usedin the drawings to identify similar elements in the drawings. Inaddition, some of the figures may have been simplified by the omissionof certain elements in order to more clearly show other elements. Suchomissions are not necessarily indicative of the presence or absence ofparticular elements in any of the exemplary embodiments, except as maybe explicitly stated in the corresponding detailed description.

FIG. 1 is a flow chart of a process for preparing high-purity taurineand salt products in accordance with one embodiment of the presentdisclosure;

FIG. 2 is a flow chart of a process for recycling cleaning water of anion exchange system in accordance with one embodiment of the presentdisclosure;

FIG. 3 is a flow chart of a process for extracting a taurine productfrom an adsorption solution in accordance with one embodiment of thepresent disclosure;

FIG. 4 is a flow chart of a process for extracting a sulfate productfrom an eluate in accordance with one embodiment of the presentdisclosure;

FIG. 5 is a schematic diagram of a production system for preparinghigh-purity taurine and salt products in accordance with one embodimentof the present disclosure; and

FIG. 6 is a structural schematic diagram of single resin column inaccordance with one embodiment of the present disclosure.

The drawings are intended to illustrate rather than limit the scope ofthe present invention. Embodiments of the present invention may becarried out in ways not necessarily depicted in the drawings. Thus, thedrawings are intended to merely aid in the explanation of the invention.Thus, the present invention is not limited to the precise arrangementsshown in the drawings.

DETAILED DESCRIPTION

The following detailed description describes examples of embodiments ofthe invention solely for the purpose of enabling one of ordinary skillin the relevant art to make and use the invention. As such, the detaileddescription and illustration of these embodiments are purelyillustrative in nature and are in no way intended to limit the scope ofthe invention, or its protection, in any manner. It should also beunderstood that the drawings are not to scale and in certain instancesdetails have been omitted, which are not necessary for an understandingof the present invention.

With reference to FIGS. 1-4 , a method for preparing taurine and saltincludes the following steps S1 to S5:

S1: Ethylene oxide is reacted with a bisulfite solution to generateisethionate. In some embodiments, the process conditions are that: theconcentration of the bisulfite solution is 25 wt % to 60 wt %, the molarratio of bisulfite to ethylene oxide is (1.03 to 1.08):1, the reactiontemperature is 50° C. to 80° C., and the pH of the reaction solution is6 to 7.

S2: The isethionate solution obtained in the step S1 is mixed withammonia (e.g., ammonia gas or ammonia water) and a metal salt to obtaina reaction solution. With respect to a mixing ratio, for 1 mol ofisethionate, an amount of ammonia greater than 14 mol is added, and anamount of the metal salt is 0.01 mol to 1.3 mol (per mol ofisethionate). After the ammonia is adsorbed until the ammonia content isgreater than 20% g/ml (i.e., 20 g/100 ml), an ammonolysis reaction isperformed. After the reaction is completed, residual ammonia gas isrecycled as a raw material for the ammonolysis reaction. The reactionsolution obtained after the ammonolysis reaction is completed issubjected to evaporation and concentration to obtain a concentratedsolution of taurine salt.

In one embodiment, the ammonolysis reaction is carried out at 150° C. to290° C., or 240° C. to 260° C., under a pressure of 10 MPa to 25 MPa for15 to 60 min, or for 40 to 50 min.

If a last mother solution (also commonly referred to as the last motherliquor) is reused in the ammonolysis step, the amount of the metal saltadded in S2 can be more, and if the last taurine mother solution is notreused, the amount of the metal salt can be reduced. For example, whenthe reaction solution in S2 is the isethionate, the ammonia and themetal salt, the molar ratio of isethionate:ammonia:metal salt can be1:(14 to 17):(0.01 to 0.05); and when the reaction solution in S2 is theisethionate, the ammonia, the metal salt and the reused last mothersolution, the molar ratio of isethionate:ammonia:metal salt can be 1:(14to 17):(0.05 to 0.3). When the isethionate is ammonium isethionate is inuse, an additional amount of the metal salt should be used, such thatthe molar ratio of the ammonium isethionate to the ammonia to the metalsalt can be 1:(14 to 17):(1.01 to 1.3).

Following evaporation and concentration of the reaction solution in S2,the concentrated sodium taurate solution obtained in step S2 has aconcentration of 10% to 35% m/v (in terms of taurine), or aconcentration of 10% to 25%. A solution added in the preparation processmay be purified water or reused cleaning water discharged from anadsorption unit of an ion exchange system.

S4: The concentrated taurine salt solution is then subjected toadsorption in an ion exchange system such that the taurine salt isconverted into taurine, followed by water cleaning, elution and watercleaning treatment of the ion exchange system. An adsorbent of the ionexchange system preferably is resin, particularly a resin with afunction that cations can be adsorbed. Suitable resins include cationexchange resins, such as cation exchange resins having a carboxylicgroup, a sulfonic group, a phosphate group, a phenolic group and similarmaterials. Alternatively, a chelating resin with the function ofadsorbing cations can also be used. The resin exchanges H+ for the metalcations in the taurine salt (e.g., sodium if the taurine salt is sodiumtaurate), with the resin adsorbing the metal cations and converting thetaurine salt into taurine.

Metal ions are adsorbed by the resin and, after adsorption, when the pHof a solution at an outlet of the adsorption unit is 4 to 10, theadsorption solution (containing primarily taurine) is collected. In theadsorbing process, part of the cations are allowed to penetrate through,i.e., metal cations which are at least equivalent in amount (on a molarbasis) to the isethionate anions present in the concentrated taurinesalt solution are allowed to penetrate through the resin to enter theadsorption solution. The content of the metal cations in the collectedadsorption solution can be 0.05% to 2% m/v, or 0.1% to 1%. Unreactedisethionate will remain in the concentrated taurine salt solution, andthe ion exchange system only adsorbs the cations (all of the anionspenetrate through). It is better to allow the metal ions which areequivalent in amount to the isethionate anions to penetrate through soas to ensure that ingredients at an adsorption solution outlet are thetaurine and the isethionate. Otherwise, adsorbing excessive or all themetal ions will result in the ingredients at the adsorption solutionoutlet to exist in a form of the taurine and isethionic acid. Isethionicacid in the ingredients is relatively unstable and is liable todeteriorate and decompose in the subsequent heating, evaporating,concentrating process. Isethionic acid is also relatively high inviscosity, which significantly influence subsequent extraction of thetaurine. In addition, isethionic acid is a medium strong acid, and undersuperacid conditions, a crystalline state of the taurine is poor,adversely affecting subsequent extraction of the taurine and reductionof the purity of the taurine.

Purified water is added into the ion exchange system for cleaningfollowing adsorption. A use volume of the purified water generally isone to two times the volume of a resin column of the ion exchangesystem, and the adsorption unit is cleaned. The cleaning water iscollected. Cleaning can be carried out until taurine cannot be detectedin the collected cleaning water. The collected cleaning water can bereused in the concentrated solution after the ammonolysis reaction.

Next, an acid used as an eluting agent is added into the ion exchangesystem, and the metal ions which have been adsorbed in the resin arecontinuously eluted. The acid may be sulfuric acid, hydrochloric acid,phosphoric acid, water-soluble carboxylic acid, sulfonic acid and thelike. The concentration of the acid added to the ion exchange system forelution is 5% to 35% m/v, or 15% to 25%. Only the cations are adsorbedin the ion exchange system, and thus, the eluted metal ions arerelatively high in purity, thereby ensuring that a salt solution with avery high purity is collected. Specifically, if the acid is the sulfuricacid, the correspondingly obtained salt is sulfate, if the acid is thehydrochloric acid, the correspondingly obtained salt is chloride, andthe sulfate and the chloride have high solubility in the water. Theeluate can be collected when the pH of the solution at an outlet of theelution unit is 2 to 8.

The elution unit is cleaned by the purified water. A use volume of thepurified water generally is one to two times the volume of the resincolumn of the ion exchange system. The cleaning water obtained afterwater cleaning is collected and is reused in the salt extractionprocess.

A cleaning mode can be adopted for both the adsorption and elutionunits, and the cleaning processes can be implemented by adopting anautomatic control system to carry out online operation, so that completeisolation between adsorption and elution can be implemented, therebyensuring complete isolation between a taurine solution in the adsorptionsolution and the salt solution in the eluate. The cleaning water can berecycled into corresponding material systems according to ingredients ofincluded materials.

A principle of ion exchange to which the present disclosure relates isillustrated as follows. In the ion exchange system, by utilizing theproperty that the ion exchange resin only adsorbs the cations, the ionexchange resin is used for adsorbing the metal cations in a material(i.e., the concentrated taurine salt solution entering the ion exchangesystem). In the adsorbing process, H⁺ is exchanged into the material soas to implement separation of the metal cations in the material andconvert the taurine salt into taurine. After adsorption is completed, bywater cleaning, it is guaranteed that there is no residual adsorptionsolution material in the ion exchange resin (e.g., taurine); and theobtained cleaning water can be reused in a production process system.The resin after cleaning contains a great amount of metal cations, anddoes not contain other components. The metal cations in the resin arethen eluted by the acid, the resin is recycled into an acid state, and acorresponding aqueous solution of the metal salt is collected. Afterelution is ended, residual acid and salt are removed up by watercleaning. After the ion exchange process is carried out, the aim ofindependently separating the taurine and the salt in two materialsystems is finally fulfilled so as to respectively carry outpurification on the taurine and the salt. In comparison, in the originalconventional process, the taurine and the salt are mixed and the twoproducts are extracted in the same material system.

Illustration will be further carried out in detail below by taking aprocess of carrying out ammonolysis to generate sodium taurate andgenerating the sodium sulfate after adding the sulfuric acid as anexample.

H₂NCH₂CH₂SO₃ ⁻Na⁺+R⁻H⁺→H₂NCH₂CH₂SO₃ ⁻H⁻+R⁻Na⁺

H₂ ⁺SO₄ ²⁻+2R⁻Na⁺→Na₂ ⁺SO₄ ²⁻+2R⁻H⁺

After the ammonolysis reaction is performed on a reaction solutionobtained after sodium hydroxyethyl sulfonate (sodium isethionate),sodium hydroxide (a metal salt) and ammonia liquor are mixed, a mainingredient in the reaction solution is sodium taurate. The reactionsolution also contains excess sodium hydroxide, a small amount of sodiumhydroxyethyl sulfonate which is not completely reacted, sodium tauratederivatives and the like. When the ammonolysis reaction is completed andthe ammonia is recycled, in the ion exchange system, a flow rate and pHare controlled so as to enable sodium ions to be adsorbed according to acertain proportion. Meanwhile, it has to be ensured that a portion ofresidual sodium ions penetrate through in the adsorption solution, sothat the main ingredients of the collected adsorption solution are thetaurine and the sodium hydroxyethyl sulfonate (sodium isethionate). Thesodium hydroxyethyl sulfonate is very high in solubility, and due tovery low content of the sodium hydroxyethyl sulfonate in the system, thesodium hydroxyethyl sulfonate cannot be separated out, so that anextraction rate of the taurine will not have the problem caused byinfluence of separation-out of the sodium sulfate in the conventionalprocess. Furthermore, due to the high solubility of the sodiumhydroxyethyl sulfonate, when solid-liquid separation is carried out, alittle residual sodium hydroxyethyl sulfonate on the surface of thetaurine can be very easily washed off in a water cleaning mode, andthus, the purity of the taurine product is also correspondinglyimproved. Thus it can be seen that according to the present disclosure,the method implements complete separation between a taurine solutionsystem and a sodium sulfate solution system by the ion exchange system,is an efficient and simple separation method, and meanwhile, alsofulfills the aim of preparing the high-purity taurine and sodiumsulfate.

S4: the adsorption solution collected in step S3 is separatelycollected, and extraction of the taurine is carried out. In theextraction process, the collected adsorption solution can be subjectedto evaporation concentration, cooling crystallization and solid-liquidseparation by adopting methods of the prior art. In one implementation,the content of the adsorption solution for evaporation concentration is25% to 40% m/v (in terms of the taurine), the cooling crystallization iscarried out at 5° C. to 30° C., the solid-liquid separation is carriedout at 5° C. to 30° C., or 15° C. to 20° C., a crude taurine product anda mother solution are obtained. The crude taurine product has a contentof over 95% taurine with a purity of 98.5% or above. The mother solutioncan be repeatedly concentrated and crystallized to extract the taurineso as to further improve the extraction rate. Main ingredients of themother solution in the taurine extraction system are the taurine and theisethionic acid metal salt. The last mother solution can be recycled asa raw material directly or after impurity removal treatment. Forexample, the last mother solution can be returned into the step S2 toparticipate in the ammonolysis reaction. In one particular embodiment,water and activated carbon are added to the obtained crude taurineproduct to be subjected to recrystallization, and after solid-liquidseparation, a finished product taurine with a higher purity is obtained.In order to better carry out recycling, the mother solution afterrecrystallization purification can be returned to the initial stage ofcarrying out evaporation concentration on the adsorption solution in thestep S4, and then concentration crystallization and separation arecarried out.

According to a specific implementation of the crude taurine productrecrystallization process, the crude taurine product is dissolved with 2to 3 times of purified water, activated carbon of which the mass is 0.1%to 0.3% of total mass of the crude product is added, decoloration iscarried out for 15 min to 40 min at a temperature of 85° C. to 98° C.,and after the activated carbon is filtered, the filtrate is cooled to atemperature of 5° C. to 30° C. or 10° C. to 20° C. for crystallization.Then, the crystallized material is dried after being separated so as toobtain the high-purity finished taurine.

S5: the material of the eluate collected in step S3 is allowed to enterthe extraction treatment process for the salt, and any one the methodsof the prior art can be adopted for this purpose. In one embodiment, thesalt is directly extracted using an evaporation crystallization process,and then solid-liquid separation is carried out. The crystallization canbe carried out at 60° C. to 125° C., or 85° C. to 110° C. After theeluate is crystallized, solid-liquid separation can be carried out at60° C. to 100° C., or 85° C. to 95° C., and the sulfate (salt) obtainedby separation has a sulfate content of over 97% and a purity of 98.5% orabove. In order to further improve the purity of the salt, the obtainedsalt also can be recrystallized.

The method for producing the high-purity taurine and salt provided bythe present disclosure can be carried out in a discontinuous,semi-continuous or continuous mode.

Certainly, as an option, the eluate collected in the step S3 can also bedirectly used as a high-purity sulfate (salt) solution.

the present disclosure also provides a production system for carryingabout the above-described process for preparing the high-purity taurineand salt. As shown in FIG. 5 and FIG. 6 , the production system includesan addition reaction device 1 for reacting the ethylene oxide and thebisulfate, an ammonolysis reaction device 2, an evaporation device 3(for concentrating the taurine salt solution following ammonolysis) anda taurine salt concentrated solution collection device 4. The taurinesalt concentrated solution collection device 4 is connected with an ionexchange system 5, such that a concentrated taurine salt solution can besupplied to the ion exchange system 5 to be subjected to ion exchange.Each device and system above are all provided with material inlets andoutlets and control valves, which are required for process demands,wherein the ammonolysis reaction device 2 is provided, for example, witha material inlet 21 for supplying the metal salt, an ammonia liquor andreused ammonia gas inlet (not shown in FIG. 5 ) and an inlet forreceiving material discharged by the addition reaction device 1.

The present disclosure can employ any existing ion exchange system, andthe structure of the ion exchange system is not limited. For example,the ion exchange system may be a fixed bed, or may also be a pulse bedor a simulated moving bed which combines a continuous countercurrentsystem technology on the basis of a conventional fixed bed resinadsorption and ion exchange process, or may be a continuous exchangebed. An existing continuous exchange bed includes a plurality of resincolumns, and can complete the whole technological processes ofadsorption, elution and water cleaning in one process cycle. Incomparison, the fixed bed carries out operations of all the steps in anintermittent process in a mode that each step is carried out separatelyfor a period of time.

In the specific embodiment shown in FIG. 5 , the ion exchange system 5includes four cation adsorption resin columns 51, 52, 53 and 54, and anelectromagnetic pump (not shown). Each resin column is provided withthree material inlets and four material outlets, and entrance and exitof the materials are controlled by valves. The three material inletsinclude concentrated solution inlets 511, 521, 531 and 541, acid inlets512, 522, 532 and 542, and purified water inlets 513, 523, 533 and 543.The material outlets include adsorption solution outlets 514, 524, 534and 544, adsorption cleaning water outlets 515, 525, 535 and 545, eluateoutlets 516, 526, 536 and 546, and elution cleaning water outlets 517,527, 537 and 547. The adsorption solution outlets 514, 524, 534 and 544are connected with a taurine extraction device 6, and the eluate outlets516, 526, 536 and 546 are connected with a salt extraction device 7. Theadsorption cleaning water outlets 515, 525, 535 and 545 are connectedwith the concentrated solution collection device 4, and the elutioncleaning water outlets 517, 527, 537 and 547 are connected with the saltextraction device 7. The material inlets and the material outlets of theresin columns are all fixed. Thus, the three material inlets for eachcolumn can share one inlet to the column, the four material outlets foreach column can share one outlet from the column, and entrance and exitswitching of each material is implemented, for example, by a valve arrayor in any one of other feasible valve control modes. When the ionexchange system comprising multiple (e.g, four) columns, the systemoperates, in any given time period the four resin columns are operatingin different process states, thereby simulating a continuous ionexchange system operational mode.

FIG. 5 depicts the working states of four resin columns 51, 52, 53 and54 in the same time period, in which processes of adsorption, watercleaning, elution and water cleaning are sequentially carried out.Specifically, the resin column 51 is in an adsorbing state, the valve ofthe concentrated solution inlet 511 is opened, the concentrated solutionin the concentration solution collection device 4 flows into the resincolumn 51, the valves of the acid inlet 512 and the purified water inlet513 are closed, at a material outlet end, the valve of the adsorptionsolution outlet 514 is opened, the taurine extraction device 6 collectsthe adsorption solution, and the valves of the adsorption cleaning wateroutlet 515, the eluate outlet 516 and the elution cleaning water outlet517 are closed. The resin column 52 is in a water cleaning state, thevalve of the purified water inlet 523 is opened, purified water isintroduced into the resin column 52, the valves of the concentratedsolution inlet 521 and the acid inlet 522 are closed, at the materialoutlet end, the valve of the adsorption cleaning water outlet 525 isopened, cleaning water flows into the concentrated solution collectiondevice 4, and the valves of the adsorption solution outlet 524, theeluate outlet 526 and the elution cleaning water outlet 517 are closed.The resin column 53 is in an eluting state, the valve of the acid inlet532 is opened, acid is introduced into the resin column 53, the valvesof the purified water inlet 533 and the concentrated solution inlet 531are closed, at the material outlet end, the eluate outlet 536 is opened,the eluate flows into the salt extraction device 7, and the valves ofthe elution cleaning water outlet 537, the adsorption solution outlet534 and the adsorption cleaning water outlet 535 are closed. The resincolumn 54 is in a water cleaning state, the valve of the purified waterinlet 543 is opened, the purified water is introduced into the resincolumn 54, the valves of the concentrated solution inlet 541 and theacid inlet 542 are closed, at the material outlet end, the valve of theelution cleaning water outlet 547 is opened, elution cleaning waterflows into the salt extraction device 7, and the valves of theadsorption solution outlet 544, the eluate outlet 546 and the adsorptioncleaning water outlet 545 are closed. Besides the equipment above, thesystem further includes a control system, power equipment, connectingparts, pipeline valves and the like which are necessary for production,all of which are common technical means in the art and are not repeatedherein. In the processes of adsorption, elution and twice water washingof the ion exchange system, separate collection of an adsorption unitand an elution unit on outlet materials can be implemented by the valvearray control system, and the outlet materials include the adsorptionsolution, the eluate and the cleaning water discharged from theadsorption unit and the elution unit.

The pH values of the outlet solutions are acquired by pH valuemonitoring devices (e.g., pH meters) arranged in the outlet of theadsorption unit and the outlet of the elution unit in the ion exchangesystem, and discharge time of the adsorption solution and the eluate areselected so as to collect an aqueous solution containing a high-puritytaurine adsorption solution material and the high-purity salt.

The taurine extraction device (or system) 6 and the salt extractiondevice (or system) 7 can include any applicable equipment and systemsknown to those skilled in the art for carrying out evaporation, coolingcrystallization (or crystallization), and solid-liquid separation. Forexample, conventional evaporation equipment, cooling crystallizationequipment/crystallization equipment and solid-liquid separationequipment can be utilized as the extraction device (i.e., extractionsystem). The solid-liquid separation equipment in the extraction devicecan include any applicable equipment known to those skilled in the artfor such use, such as a panel centrifuge, a top-suspended centrifuge, acontinuous horizontal spiral centrifuge, a plate-and-frame filter pressand the like.

As shown in the alternative embodiment of FIG. 6 , if only one resincolumn 55 is included in the ion exchange system, the system similarlyincludes three material inlets 551, 552 and 553 and four materialoutlets 554, 555, 556 and 557, the three material inlets can share oneinlet of the column 55, the four material outlets can share one outletof the column 55, the ion exchange system is controlled by the valves tosequentially proceed to different working states of adsorption, watercleaning, elution and water cleaning in an intermittent operating mode.

In order to illustrate the technical effects of the preparation methoddisclosed by the present disclosure, the following examples are used forillustration. Unless otherwise specified, raw materials used in thefollowing embodiments are all commercially available products. Unlessotherwise specified, the individual steps used in the followingembodiments are all conventional steps; and unless otherwise specified,the material content all refers to percentage by mass volume.

Example 1

This example shows a preparation process of an ammonolysis solution.

Preparation of sodium hydroxyethyl sulfonate (sodium isethionate):sodium bisulfite and ethylene oxide are mixed according to a molar ratioof the sodium bisulfite to the ethylene oxide of 1.05:1, and the mixtureis subjected to a reaction under the conditions of a pH value of 6.2 to6.8 and a temperature of 60° C. to 65° C. so as to obtain sodiumhydroxyethyl sulfonate.

Preparation of ammonolysis solution: the sodium hydroxyethyl sulfonate,sodium hydroxide (i.e., a metal salt) and ammonia are subjected to areaction for 45 min under the conditions of a temperature of 255° C. anda pressure of 10 MPa to 18 MPa. After the reaction is completed, ammoniagas is discharged and recycled, and concentration is carried out toobtain a concentrated ammonolysis reaction solution (i.e., aconcentrated sodium taurate solution).

Example 2

This example shows that the ion exchange system adsorbs the sodium ionsfrom the sodium taurate in the concentrated ammonolysis reactionsolution and implements separation in two material solution systems forthe taurine and the sodium sulfate (salt).

The concentrated ammonolysis solution is prepared into an 18 L ofsolution in which the taurine content of the solution is 20% (m/v). 12 Lof sulfuric acid solution with a concentration of 15% m/v is prepared.In a small-sized ion exchange system having a resin adapted for sodiumion adsorption, the prepared taurine solution is pumped into the system.The pH of the collected adsorption solution is controlled within a rangeof 7 to 8 (by controlling the amount of the taurine solution), thecontent of the sodium ions in the adsorption solution is 0.05% to 1%m/v, 22 L of adsorption solution is collected in total, the taurinecontent is 16%, and the sodium hydroxyethyl sulfonate (sodiumisethionate) content is 1.5%. The system is then cleaned with purifiedwater, and the cleaning water is collected and reused in theconcentrated ammonolysis solution, and cleaning is carried out untiltaurine cannot be detected in the collected cleaning water leaving theion exchange system. Next, the sulfuric acid solution with aconcentration of 15% is pumped into the cleaned ion exchange system. ThepH of the collected eluate is controlled within a range of about 3 to 5(by controlling the amount of sulfuric acid), and 16 L of eluate ofwhich the sodium sulfate content is 17% is collected in total. Aftereluate collection is completed, the ion exchange system is once againcleaned with purified water, and the cleaning water is discharged fromthe ion exchange system, so that a cyclic adsorbing and separatingfunction can be achieved. The system can implement continuous feedingand discharging control, for example, by adopting a plurality of resincolumns, thereby ensuring stability of the material content of thedifferent collected solutions.

Items Adsorption Solution Eluate Taurine Content (g/ml)   16% less than1 ppb Sodium Hydroxyethyl Sulfonate 1.50% less than 1 ppb Content (g/ml)Sodium Sulfate Content (g/ml) smaller than 10 ppm 17%

Example 3

This embodiment shows a process (e.g., FIG. 2 and FIG. 3 ) ofrespectively carrying out concentration extraction on the adsorptionsolution and the eluate which are collected in Example 2.

(1) Extraction of the adsorption solution: 3 L of adsorption solution istaken and concentrated to a taurine concentration of 33%, and cooling iscarried out to a temperature of 15° C. to carry out centrifugalseparation so as to obtain a crude taurine product with a taurinecontent of 95.5% (g/g) and moisture content of 3.5% (g/g). When moistureis removed, the taurine content is 98.96% (g/g), and the purity is veryhigh. After the taurine is extracted, in the mother solution, thetaurine content is 10%, the sodium hydroxyethyl sulfonate content is4.7%, and the sulfate content is less than 10 ppm.

(2) Extraction of the eluate: 3 L of eluate is taken, subjected tosix-time concentration crystallization at a high temperature of 95° C.and subjected to centrifugal separation to obtain sodium sulfate (salt)with a sodium sulfate content of 97.5% (g/g) and a moisture content of2.0% (g/g). After the moisture is removed, the sodium sulfate content is99.49% (g/g), and the purity is very high. In the mother solution, thetaurine content is less than 1 ppb, the sodium hydroxyethyl sulfonatecontent is less than 1 ppb, and the sulfate content is 35%.

Extraction of Taurine from Extraction of Sodium Sulfate AdsorptionSolution from Eluate Taurine Content (g/g) 95.50% <1 ppb SodiumHydroxyethyl Sulfonate <0.05% <1 ppb Content (g/g) Sodium SulfateContent (g/g) <10 ppm 97.50% Moisture Content(g/g)  3.50%  2.00% PurityAfter Removal of Moisture 98.96% 99.49%

Mother Solution Mother Solution after Extraction after Extraction of ofTaurine Sodium Sulfate Taurine Content (g/ml)   10% <1 ppb SodiumHydroxyethyl Sulfonate Content (g/ml) 4.70% <1 ppb Sodium SulfateContent (g/ml) <10 ppm 35%

Example 4

This example shows a process of respectively carrying outrecrystallization on the taurine and the sodium sulfate.

Recrystallization of the taurine: 200 g of the crude taurine productcollected in Example 3 is taken, 500 g of purified water is added, 0.4 gof activated carbon is added. The mixture is heated to a temperature of95° C., and the temperature is maintained for 20 min. Thereafter theactivated carbon is removed by filtration, cooling is carried out to atemperature of 15° C. to carry out crystallization, the crystallizationsolution is separated, and after drying, 155 g of dry fine taurineproduct is obtained. The fine mother solution obtained by separation canbe recycled and reused in the previous process which may be theconcentration crystallization process, or can be returned into a nextbatch of materials in the recrystallization process. Detected data is asfollows:

High-Purity Fine Product Items Taurine Appearance: white crystalparticles, no odor and tartish taste Content(C2H7NSO3): 99.9% ChloridePPM: <10 ppm Sulfate PPM: <10 ppm Ammonium Salt PPM: <10 ppm Residues onIgnition: 0.005% Loss on Drying:  0.05% Heavy Metal (in terms  <1 ppm ofPb): Arsenic Salt (in terms  <1 ppm of As):

Recrystallization of the sodium sulfate: 200 g of sodium sulfatecollected in Example 3 is taken, 500 g of purified water is added,heating is carried out to a temperature of 95° C. to carry outevaporation crystallization, the crystallization solution is separated,and after drying, 190 g of dry fine sodium sulfate (salt) is obtained.The mother solution obtained by separation can be recycled and reused inthe previous process, i.e., the concentration crystallization process,or can be returned into a next batch of materials in therecrystallization process.

Detected data is as follows:

High-Purity Fine Product Items Sodium Sulfate Appearance: white crystalparticles Content(Na2SO4): 99.90% Chloride PPM: <10 ppm Moisture Content 0.02% Heavy Metal (in terms of Pb): <1 ppm Arsenic Salt (in terms ofAs): <1 ppm

Example 5 (Prior Art)

This example shows a conventional method for producing and separatingthe taurine and the sodium sulfate.

Extraction of the taurine: after the ammonolysis concentrated solutionis prepared into a certain concentration, under the stirring condition,concentrated sulfuric acid is slowly added for neutralization, atemperature in the neutralizing process is controlled within a range of50° C. to 60° C., when pH is 8.0, the addition of the acid is stopped,cooling is carried out to a temperature of 33° C. to carry outcrystallization, and separation is carried out to obtain a crude taurineproduct and a mother solution. In the crude product, the taurine contentis 90% (g/g), the sodium sulfate content is 3% (g/g) and the moisturecontent is 6%. In the mother solution, the taurine content is 15%, andthe sulfate content is 25%.

Extraction of the sodium sulfate: the mother solution obtained after thetaurine is extracted is concentrated again to a concentration of 33%sodium sulfate, the sodium sulfate is separated at a high temperature of95° C. or above, and in the product obtained by separation, the sodiumsulfate content is 90% (g/g), the moisture content is 5%, and thetaurine content in the sulfate is 4%. The mother solution subjected toseparation is cooled to a temperature of 33° C. to extract the taurine,and separation and extraction of the sodium sulfate and the taurine arerepeatedly carried out in this way.

Extraction of Extraction of Taurine by Sodium sulfate ConventionalProcess by Conventional Process Taurine Content (g/g) 90.00%     4%Sodium Hydroxyethyl Sulfonate <0.05%  <0.1% Content (g/g) Sodium SulfateContent(g/g)     3% 90.00% Moisture Content (g/g)     6%  5.00% PurityAfter Removal of Moisture 95.74% 94.74%

Example 6

This example shows that the ion exchange system adsorbs the sodium ionsand implements separation into two material solution systems of thetaurine and the salt (in this instance, sodium chloride).

A concentrated ammonolysis solution is prepared into 18 L of solution inwhich the taurine content is 20%. 24 L of hydrochloric acid solutionwith a concentration of 12% is prepared. The prepared taurine solutionis pumped into the ion exchange system. The pH of the collectedadsorption solution is controlled within a range of 7 to 8, the contentof the sodium ions in the adsorption solution is 0.05% to 1%, 22 L ofadsorption solution is collected in total, the taurine content is 16%,and the sodium hydroxyethyl sulfonate content is 1.5%. The system iscleaned with purified water, the cleaning water is collected and reusedin a material of the concentrated ammonolysis solution, and cleaning iscarried out until taurine cannot be detected in the collected cleaningwater. Next, the hydrochloric acid solution with a concentration of 12%is pumped into the cleaned system. The pH of the collected eluate iscontrolled within a range of about 3 to 5, and 28 L of eluate of whichthe sodium chloride content is 17% is collected in total. Aftercollection is completed, the system is cleaned with the purified water.

Items Adsorption Solution Eluate Taurine Content (g/ml)   16% <1 ppbSodium Hydroxyethyl Sulfonate 1.50% <1 ppb Content(g/ml) Sodium ChlorideContent (g/ml) <10 PPm 17%

By the embodiments above, it can be obviously seen that in theconventional process, the taurine and the sodium sulfate of the materialsystems are mixed together, resulting in that the product content of theextracted and separated taurine and sodium sulfate is relatively low,the moisture content is high, the purities are poor, and meanwhile, theprocess of process control is relatively complex. Preparation accordingto the method disclosed by the present disclosure essentially solves theproblem of a case that the taurine and sodium sulfate/sodium chloridematerial systems are mixed together to be subjected to extraction andseparation, and fulfills the aim of preparing the high-purity taurineand sodium sulfate/sodium chloride.

Finally, it should be noted that the embodiments above are merely usedfor illustrating the technical solutions of the present disclosure, butnot intended to limit the present disclosure. Although the presentdisclosure has been illustrated in detail with reference to theabove-mentioned embodiments, those of ordinary skill in the art willunderstand that they still can make modifications to the technicalsolutions described in the above-mentioned embodiments, or replacepreparation reaction conditions, or make equivalent replacements to partof the technical characteristics, and those modifications orreplacements will not enable the essences of the corresponding technicalsolutions to depart from the spirit and scope of the technical solutionsof the embodiments of the present disclosure.

While various embodiments of the present disclosure have been describedin detail above, it will be understood that the components, features andconfigurations, as well as the methods of manufacturing the devices andmethods described herein are not limited to the specific embodimentsdescribed herein.

What is claimed is:
 1. A system for preparing high-purity taurine and salt for use in producing the taurine by an ethylene oxide synthesis method, the system comprising: (a) an addition reaction device; (b) an ammonolysis reaction device; (c) an evaporation device; and (d) a taurine salt concentrated solution collection device; wherein the ammonolysis reaction device is provided with a metal salt inlet, the taurine salt concentrated solution collection device is connected with an ion exchange system for ion exchange, the ion exchange system is provided with an acid inlet, an adsorption solution outlet and an eluate outlet, the adsorption solution outlet of the ion exchange system is connected with a taurine extraction device, the eluate outlet of the ion exchange system is connected with a salt extraction device, and further wherein the ion exchange system is provided with a purified water inlet, an adsorption unit cleaning water outlet and an elution unit cleaning water outlet.
 2. The system according to claim 2, wherein the adsorption unit cleaning water outlet is connected with the taurine salt concentrated solution collection device, and the elution unit cleaning water outlet is connected with the salt extraction device. 